Ethyl acetate differential pressure rectification production line

Abstract

The utility model discloses an ethyl acetate differential pressure rectification production line which comprises a dehydration refining tower, and a crude fat inlet and a dehydration steam outlet are formed in the dehydration refining tower; the recovery tower is provided with a water phase inlet and a recovered steam inlet, and the dehydrated steam outlet is communicated with the recovered steam inlet through a recovery tower reboiler; the output end of the water-phase preheating unit is communicated with the water-phase inlet; the input end of the wastewater recycling unit is communicated with the wastewater outlet of the recycling tower, and the output end is communicated with the water-phase preheating unit; an ester phase outlet of the recovery tower is communicated with the dehydration refining tower through the ester phase reflux unit. The water phase of the recovery tower needs to be preheated by the water phase preheating unit before being input, and the wastewater in the wastewater recovery unit can be directly used as a heat source of the water phase preheating unit to directly preheat the water phase, so that the reuse of the wastewater is realized, and the waste of water is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to ethyl acetate production technical field especially relates to a kind of ethyl acetate differential pressure rectification production line. BACKGROUND

[0002] Ethyl acetate is also called ethyl acetate, pure ethyl acetate is colorless transparent liquid with pungent smell, is a kind of fine chemical products with wide application, has excellent solubility, fast drying, is widely used, is a very important organic chemical raw material and excellent industrial solvent, is widely used in the production process of acetate fiber, ethyl fiber, chlorinated rubber, ethylene resin, acetate fiber resin, synthetic rubber, paint and paint etc.Ethyl acetate is obtained in the production line of ethyl acetate, and part of crude fat needs to continue to carry out dehydration rectification operation, that is, to be transported to dehydration tower, water, alcohol and ester are transported to recovery tower in the form of azeotrope at the top of dehydration tower, and ester phase continues to flow back to dehydration tower after treatment, and a large amount of waste water produced at the bottom of recovery tower is directly discharged, causing a large amount of water resource waste. SUMMARY

[0003] The utility model aims at at least solving one of the above-mentioned technical problems, provide a kind of ethyl acetate differential pressure rectification production line, can effectively utilize the waste water discharged by recovery tower, for the preheating treatment of water phase input recovery tower.

[0004] To achieve the above object, the technical scheme adopted by the utility model is:

[0005] A kind of ethyl acetate differential pressure rectification production line, including dehydration refining tower, the dehydration refining tower is equipped with crude fat inlet and dehydration steam outlet;Recovery tower, the recovery tower is equipped with water phase inlet and recovery steam inlet, and the dehydration steam outlet is connected with the recovery steam inlet by recovery tower reboiler;Water phase preheating unit, its output end is connected with water phase inlet;Waste water recovery unit, its input end is connected with the waste water outlet of recovery tower, and output end is connected with water phase preheating unit;Ester phase reflux unit, the ester phase outlet of the recovery tower is connected with the dehydration refining tower by ester phase reflux unit.

[0006] As the improvement of the above technical scheme, the water phase preheating unit includes recovery tower feed preheater, the water phase outlet of the ester phase reflux unit and the water phase outlet of ethyl acetate esterification production line are connected with the input end of recovery tower feed preheater by dehydration water washing pump, and the output end of the waste water recovery unit is connected with recovery tower feed preheater.

[0007] As the improvement of the above technical scheme, the waste water recovery unit includes waste water tank, the waste water outlet of the recovery tower is connected with the input end of waste water tank, and the output end of the waste water tank is connected with recovery tower feed preheater by waste water pump.

[0008] As the improvement of the above technical scheme, the ester phase reflux unit comprises a dehydration column condenser, an input end of the dehydration column condenser being communicated with a recovery column reboiler, a dehydration column reflux preheater being communicated with an output end of the dehydration column condenser, a dehydration column cooler being communicated with an output end of the dehydration column reflux preheater, a dehydration column water washing mixer being communicated with an output end of the dehydration column cooler, and a dehydration column fractionator being communicated with an output end of the dehydration column water washing mixer through a dehydration column reflux pump.

[0009] As the improvement of the above technical scheme, a dehydration column feed preheater is communicated with a crude fat inlet of the dehydration refining column, and a dehydration column reboiler is communicated with a bottom of the dehydration refining column.

[0010] As the improvement of the above technical scheme, a product output end of the dehydration refining column is communicated with a product extraction pump, an output end of the product extraction pump is communicated with a product cooler, and an output end of the product cooler is communicated with a product intermediate tank.

[0011] As the improvement of the above technical scheme, the recovery column separation unit comprises a recovery column condenser, an input end of the recovery column condenser being communicated with a recovery column steam outlet, and a recovery column separator being communicated with an output end of the recovery column condenser.

[0012] As the improvement of the above technical scheme, a water phase outlet at a bottom of the recovery column separator is communicated with a recovery column reflux tank, and an output end of the recovery column reflux tank is communicated with the recovery column through a reflux pump.

[0013] As the improvement of the above technical scheme, a steam outlet at a top of the recovery column separator is communicated with a jet pump, a circulating cooler is communicated with a top of the jet pump, a water circulating tank is communicated with a bottom of the jet pump, and a bottom of the circulating cooler is communicated with the water circulating tank through a circulating water pump.

[0014] Compared with the prior art, the application has the following beneficial effects:

[0015] The crude fat prepared through the esterification production line enters the dehydration refining column through the crude fat inlet, and the azeotrope formed by the product, water, alcohol and ester is output from the dehydration steam outlet to the recovery column after being treated by the dehydration refining column, and the ester phase and waste water are obtained after being treated by the recovery column, wherein the ester phase is sent back to the dehydration refining column through the ester phase reflux unit, and the waste water enters the waste water recovery unit, and the water phase needs to be preheated by the water phase preheating unit before being input into the recovery column, and the waste water in the waste water recovery unit can be directly used as the heat source of the water phase preheating unit to preheat the water phase, thereby realizing the reuse of the waste water and reducing the waste of water. BRIEF DESCRIPTION OF DRAWINGS

[0016] The specific embodiments of the present application will be further described in conjunction with the drawings, in which:

[0017] Figure 1 is a production line structure schematic diagram of the embodiment of the present application;

[0018] Figure 2 is a production line structure schematic diagram of the embodiment of the present application; Figure One

[0019] Figure 3 is a production line structure schematic diagram of the embodiment of the present application; Figure Two

[0020] Figure 4 is a production line structure schematic diagram of the embodiment of the present application; Figure Three DETAILED DESCRIPTION

[0021] The technical solutions in the embodiments of the present application will be described clearly and completely in conjunction with the drawings of the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, but not all the embodiments. Based on the embodiments of the present application, all the other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.

[0022] It should be noted that when a component is referred to as being "fixed" to another component, it can be directly on the other component or there can be intervening components. When a component is referred to as being "connected" to another component, it can be directly connected to the other component or there can be intervening components. When a component is referred to as being "disposed on" another component, it can be directly disposed on the other component or there can be intervening components. When a component is referred to as being "disposed in the middle", it is not only disposed in the middle position, but also disposed in the range defined by the two ends. The terms "vertical", "horizontal", "left", "right", and similar terms used herein are for illustrative purposes only.

[0023] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used in the description of the application herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used in this description, the term "and / or" includes any and all combinations of one or more of the associated listed items.

[0024] As Figures 1 to 4 ​​​The utility model provides a kind of ethyl acetate differential pressure rectification production line, including dehydration refining tower 10, the dehydration refining tower 10 is equipped with crude fat inlet 11 and dehydration steam outlet 12;Recovery tower 20, the recovery tower 20 is equipped with water phase inlet 21 and recovery steam inlet 22, the dehydration steam outlet 12 is connected by recovery tower reboiler 23 recovery steam inlet 22;Water phase preheating unit 30, its output end is connected with water phase inlet 21;Waste water recovery unit 40, its input end is connected with the waste water outlet 24 of recovery tower 20, and output end is connected with water phase preheating unit 30;Ester phase reflux unit 50, the ester phase outlet 25 of recovery tower 20 is connected by ester phase reflux unit 50 dehydration refining tower 10. Among them, the crude fat of the esterification production line of ethyl acetate is entered dehydration refining tower 10 from middle crude fat inlet 11, the dehydration steam outlet 12 is equipped at dehydration refining tower 10 top, azeotrope formed by water, alcohol and ester is discharged to recovery tower 20, and qualified product in dehydration refining tower 10 is directly output storage;The ester phase obtained in the recovery tower 20 is sent back to dehydration refining tower 10 by ester phase reflux unit 50, and waste water enters waste water recovery unit 40.

[0025] Referring to Figure 1 And Figure 4 In the specific embodiment of the present application, the water phase preheating unit 30 includes recovery tower feed preheater 31, the water phase outlet of ester phase reflux unit 50 and the water phase outlet of ethyl acetate esterification production line are both connected with the input end of recovery tower feed preheater 31 through dehydration water washing pump 32, and the output end of waste water recovery unit 40 is connected with recovery tower feed preheater 31. In addition, the waste water recovery unit 40 includes waste water tank 41, the waste water outlet 24 of recovery tower 20 is connected with the input end of waste water tank 41, and the output end of waste water tank 41 is connected with recovery tower feed preheater 31 through waste water pump 42. Among them, the input electric control valve on the input end of waste water tank 41 is interlocked with recovery tower 20, and when the waste water in recovery tower 20 reaches a certain height, the automatic electric control valve is opened to discharge into waste water tank 41.

[0026] Referring to Figure 1 And Figure 3In the detailed description of the present application, the ester phase reflux unit 50 comprises a dehydration column condenser 51, the input end of which is connected to the recovery column reboiler 23, and the output end of which is connected to a dehydration column reflux preheater 52, the output end of which is connected to a dehydration column cooler 53, the output end of which is connected to a dehydration column water washing mixer 54, the output end of which is connected to a dehydration column fractionator 55, and the output end of which is connected to the dehydration purification column 10 through a dehydration column reflux pump 56. The dehydration column condenser 51 is connected to a circulating cooling water pipe. After the ester phase is washed by condensing water, the upper ester is refluxed into the dehydration purification column 10, and the lower water is sent to the recovery column 20 through the water phase preheating unit 30.

[0027] Referring to Figure 1 and Figure 2 In the detailed description of the present application, the crude fat inlet 11 of the dehydration purification column 10 is connected to a dehydration column feed preheater 13, and the bottom of the dehydration purification column 10 is connected to a dehydration column reboiler 14. The dehydration column reboiler 14 is connected to the bottom of the column, and a steam pipe is connected to the top of the column, which can heat and vaporize the liquid at the bottom of the column. Further, the output end of the dehydration purification column 10 is connected to a product extraction pump 15, the output end of which is connected to a product cooler 16, and the output end of which is connected to a product intermediate tank 17. The product cooler 16 is connected to a circulating cooling water pipe.

[0028] Referring to Figure 1 and Figure 4 In the detailed description of the present application, a recovery column separation unit 60 is further included, the recovery column 20 is provided with a recovery column steam outlet 26, and the recovery column separation unit 60 comprises a recovery column condenser 61, the input end of which is connected to the recovery column steam outlet 26, and the output end of which is connected to a recovery column separator 62. The water phase outlet at the bottom of the recovery column separator 62 is connected to a recovery column reflux tank 63, the output end of which is connected to the recovery column 20 through a reflux pump 64. The steam outlet at the top of the recovery column separator 62 is connected to a jet pump 65, the top of which is connected to a circulating cooler 66, and the bottom of which is connected to a water circulation tank 67, which is connected to the bottom of the circulating cooler 66 through a circulating water pump 68.

[0029] In addition, the tail gas output ends of the dehydration fractionator 55, the recovery column reflux tank 63 and the circulating water tank 67 are all connected to a tail gas treatment device.

[0030] The crude ester prepared through the esterification production line enters the dehydration refining tower 10 through the crude ester inlet 11, and the azeotrope formed by the finished product, water, alcohol and ester is output from the dehydration steam outlet 12 to the recovery tower 20 after being treated by the dehydration refining tower 10, and the ester phase and waste water are obtained after being treated by the recovery tower 20, wherein the ester phase is sent back to the dehydration refining tower 10 through the ester phase reflux unit 50, and the waste water enters the waste water recovery unit 40, and the water phase of the recovery tower 20 needs to be preheated by the water phase preheating unit 30 before being input, and the waste water in the waste water recovery unit 40 can be directly used as the heat source of the water phase preheating unit 30 to preheat the water phase, so that the waste water is reused, and the waste of water is reduced.

[0031] The above examples are only used to illustrate the technical scheme of the utility model and not to limit it, and any modification or equivalent replacement without departing from the spirit and scope of the utility model should be covered in the scope of the technical scheme of the utility model.

Claims

1. An ethyl acetate differential pressure rectification production line, characterized in that, comprising dehydration refining column, which is provided with a crude fat inlet and a dehydration vapor outlet; recovery column, which is provided with a water phase inlet and a recovery vapor inlet, and the dehydration vapor outlet is connected to the recovery vapor inlet through a recovery column reboiler; water phase preheating unit, which is connected to the water phase inlet; waste water recovery unit, which is connected to the waste water outlet of the recovery column at the input end and connected to the water phase preheating unit at the output end; ester phase reflux unit, which is connected to the dehydration refining column at the ester phase outlet.

2. The ethyl acetate differential pressure rectification production line according to claim 1, characterized in that, The water phase preheating unit comprises a recovery column feed preheater, the water phase outlet of the ester phase reflux unit and the water phase outlet of the ethyl acetate esterification production line are both connected to the input end of the recovery column feed preheater through a dehydration water washing pump, and the output end of the waste water recovery unit is connected to the recovery column feed preheater.

3. The ethyl acetate differential pressure rectification production line according to claim 2, characterized in that, The waste water recovery unit comprises a waste water tank, the waste water outlet of the recovery column is connected to the input end of the waste water tank, and the output end of the waste water tank is connected to the recovery column feed preheater through a waste water pump.

4. The ethyl acetate differential pressure rectification production line according to claim 1, characterized in that, The ester phase reflux unit comprises a dehydration column condenser, the input end of the dehydration column condenser is connected to the recovery column reboiler, the output end of the dehydration column condenser is connected to a dehydration column reflux preheater, the output end of the dehydration column reflux preheater is connected to a dehydration column cooler, the output end of the dehydration column cooler is connected to a dehydration column water washing mixer, the output end of the dehydration column water washing mixer is connected to a dehydration column delayer, and the output end of the dehydration column delayer is connected to the dehydration refining column through a dehydration column reflux pump.

5. The ethyl acetate differential pressure rectification production line according to claim 1, characterized in that, The crude fat inlet of the dehydration refining column is connected to a dehydration column feed preheater, and the bottom of the dehydration refining column is connected to a dehydration column reboiler.

6. The ethyl acetate differential pressure rectification production line according to claim 5, characterized in that, The product output end of the dehydration refining column is connected to a product production pump, the output end of the product production pump is connected to a product cooler, and the output end of the product cooler is connected to a product intermediate tank.

7. The ethyl acetate differential pressure rectification production line according to claim 1, characterized in that, Further comprising a recovery column separation unit, which is provided with a recovery column vapor outlet, and the recovery column separation unit comprises a recovery column condenser, the input end of the recovery column condenser is connected to the recovery column vapor outlet, and the output end of the recovery column condenser is connected to a recovery column separator.

8. The ethyl acetate differential pressure rectification production line according to claim 7, characterized in that, The water phase outlet at the bottom of the recovery column separator is connected to a recovery column reflux tank, and the output end of the recovery column reflux tank is connected to the recovery column through a reflux pump.

9. The ethyl acetate differential pressure rectification production line according to claim 7, characterized in that, The vapor outlet at the top of the recovery column separator is connected to an injection pump, the top of the injection pump is connected to a circulating cooler, the bottom of the injection pump is connected to a water circulation tank, and the water circulation tank is connected to the bottom of the circulating cooler through a circulating water pump.

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